EP2078555B1 - Procédé et installation de nettoyage de gaz d'échappement - Google Patents

Procédé et installation de nettoyage de gaz d'échappement Download PDF

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Publication number
EP2078555B1
EP2078555B1 EP08000447.6A EP08000447A EP2078555B1 EP 2078555 B1 EP2078555 B1 EP 2078555B1 EP 08000447 A EP08000447 A EP 08000447A EP 2078555 B1 EP2078555 B1 EP 2078555B1
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EP
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Prior art keywords
reactor
sorbent
exhaust gases
sorption
fresh
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Not-in-force
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EP08000447.6A
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German (de)
English (en)
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EP2078555A1 (fr
Inventor
Philipp Oliver Morf
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Hitachi Zosen Innova AG
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AE&E Inova AG
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Priority to PL08000447T priority Critical patent/PL2078555T3/pl
Priority to DK08000447.6T priority patent/DK2078555T3/da
Priority to EP08000447.6A priority patent/EP2078555B1/fr
Priority to PCT/EP2009/000072 priority patent/WO2009087100A1/fr
Publication of EP2078555A1 publication Critical patent/EP2078555A1/fr
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Publication of EP2078555B1 publication Critical patent/EP2078555B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B01D53/12—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/81—Solid phase processes
    • B01D53/83—Solid phase processes with moving reactants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L7/00—Supplying non-combustible liquids or gases, other than air, to the fire, e.g. oxygen, steam
    • F23L7/002—Supplying water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2047—Hydrofluoric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/60—Sorption with dry devices, e.g. beds

Definitions

  • the present invention relates to a method for purifying exhaust gases according to claim 1, an exhaust gas purification system according to claim 8, as well as the use of this exhaust gas purification system according to claim 11.
  • Waste gases which are produced during waste incineration, for example, are generally cleaned by removing pollutants such as HCl, HF, SO 2 , nitrogen oxides and dioxin as well as dusts contained therein in an emission control system.
  • pollutants such as HCl, HF, SO 2 , nitrogen oxides and dioxin as well as dusts contained therein in an emission control system.
  • a possible method for the separation of pollutants from the exhaust gases is the dry or quasi-dry sorption of pollutants by means of a sorbent. Such a method is in DE-A-32 35 559 described.
  • the exhaust gas scrubbing such as in Thomé-Kozmiensky, Karl J .: Thermal Waste Treatment, EF-Verlag for Energy and Environmental Technology, Berlin 1994 (pages 486 - 489 ) is an alternative method of treating exhaust gases.
  • a sorbent In dry or quasi-dry sorption, a sorbent is generally introduced into a fluidized bed reactor, where it is brought into contact with the exhaust gas in a circulating fluidized bed. The pollutants sorb on the sorbent.
  • the fluidized bed reactor is usually followed by a solids separator. In this entrained in the exhaust solids and thus also loaded with pollutant sorbent are deposited. The secluded Solids are either discharged or returned to the fluidized bed reactor.
  • a corresponding method is in EP-B-1 537 905 described.
  • FR-A-2 722 113 discloses a method of treating waste gases from a waste incineration plant having two series-arranged operating stages, each comprising a reactor and a dust extractor, and wherein fresh reagent is introduced in at least one stage.
  • DE-A-1444974 discloses a process for the desulfurization of industrial gases using a hot fluidized bed arranged in an absorption vessel, which consists of oxide, which continuously circulates between the absorption vessel and a vessel for regenerating the oxide.
  • EP-A-0 550 905 discloses a method for reducing N 2 O emissions in exhaust gases released in the combustion of nitrogen-containing fuels in a fluidized bed combustion reactor.
  • US-B-5,885,539 discloses a method for separating fluorine-containing substances from a gaseous medium in a dry adsorption process.
  • the method comprises the step of treating the gas with countercurrent particulate alumina in a dry adsorption process.
  • EP-A-0694328 describes a method for separating HF, HCl, SO 2 , polyhalogenated hydrocarbons, Hg, mercury compounds and dust from an exhaust gas, the method comprising the steps of disposing of the contaminated exhaust gas in a reactor having an absorp tion medium is brought into contact, the gas-solid suspension is then passed into a pre-separator, in which the deposition of most of the solids takes place, and the pre-cleaned gas-solid suspension is then passed into a final separator, in which the entire amount introduced the absorbent and the suspended solids are separated.
  • the process of the present invention includes both dry sorption and semi-dry sorption processes.
  • the exhaust gases are introduced into a first reactor and passed from there into a downstream second reactor.
  • the exhaust gases are purified by means of a dry or quasi-dry sorption process.
  • Fresh sorbent is supplied only in the second reactor and passed from the second reactor at least partially into the first reactor.
  • the exhaust gases are preferably passed into a downstream Feststoffabscheider, where, in particular by a fabric filter, the remaining solids in the gas stream are deposited.
  • the purified gas can be removed. Sorbent deposited in the solids separator may be passed into the first reactor or removed from the system.
  • the use according to the invention of two successive reactors improves the removal of pollutants from the sorbent.
  • the second reactor leads to a better Schadstoffsorption after the (first) reactor, since the gas-solid mixture is mixed better than if it, as previously customary, is passed directly to a solids separator.
  • the fresh sorbent is supplied only in the second reactor.
  • the fresh sorbent is thus used for further purification of the exhaust gas stream, which has already been purified in the first reactor.
  • the exhaust gas flow in the second reactor has only a relatively low pollutant concentration (measurements show that about 98% of by Sorptionsvin deposited pollutants on exit from the fluidized bed reactor), which usually reduces the rate of sorption. This is particularly true when the sorbent is not fresh and has already formed on the particles a layer of reaction products resulting from the sorption of pollutants. It is believed that this layer prevents the particles from binding other pollutants.
  • the use of fresh sorbent in the second reactor accelerates sorption and improves pollutant removal. Compared to the common methods, the same cleaning performance can be achieved faster and with a smaller amount of sorbent, since the fresh sorbent is more reactive than already used.
  • the sorbent from the second reactor is passed at least partially into the first reactor.
  • its sorption capacity can be optimally utilized:
  • the sorbent When used in the second reactor, the sorbent generally absorbs only relatively small amounts of pollutants due to the low pollutant content of the exhaust gases in this area. Its sorption capacity is therefore not fully utilized in the second reactor.
  • the total amount of sorbent needed By at least partial use of the sorbent from the second reactor in the first reactor, the total amount of sorbent needed can be reduced. Due to the relatively high pollutant concentration of the exhaust gases in the first reactor also the capacity of the sorbent can be better utilized.
  • the inventive method can be used in particular for the purification of exhaust gases from a waste incineration plant.
  • sorbent which has already been used in the second reactor is used in the first reactor.
  • Spent sorbent from the first reactor can be fed to the exhaust stream into the second reactor or removed from the system, for example via a lock.
  • a fluidized bed reactor is used as the first reactor.
  • the sorbent is present in the form of a circulating fluidized bed (also referred to as "circulating fluidized bed”), which is achieved in that the solid particles contained in the exhaust gas including the supplied sorbent by the upward flow of the exhaust gas in a floating state.
  • circulating fluidized bed By chemical reaction with the sorbent in the circulating fluidized bed, the pollutants contained in the exhaust gas are deposited on the sorbent particles.
  • water is injected into the first reactor - a fluidized-bed reactor.
  • the exhaust gas temperature can be controlled in the reactor.
  • the temperature in the reactor can be kept constant at a certain value.
  • the temperature in the first reactor is maintained at a value of about 140-150 ° C.
  • the injection of water also leads to a positive effect on Schadstoffsorption: By wetting the sorbent its sorption capacity is improved.
  • the second reactor used is a fly-flow reactor, in particular a downcomer reactor.
  • a downcomer reactor is described in Zenklusen, Fabian: Formation of homogeneous gas-solid suspensions for downdraft reactors at high speeds, thesis ETH No. 12810 (pages 9 and 11-15).
  • the geometry of downcomer reactors can be chosen so that the dispersion of the circulated sorbent can be optimally designed. Through the use of fresh sorbent and its good dispersion in the second reactor, the Schadstoffsorption is optimized in the inventive process.
  • the fresh sorbent is introduced into the second reactor via a Venturi nozzle.
  • a Venturi nozzle allows optimal mixing of exhaust gases and sorbents. By the achieved improvement of the dispersion, an improved sorption of the pollutants contained in the exhaust gases is achieved.
  • a calcium, sodium, mineral and / or carbon based sorbent is used for the process of the present invention.
  • Lime hydrate (Ca (OH) 2 ) usually indicates a purity of at least 92% and a specific surface area of at least 15 m 2 / g.
  • sorbents such as sodium bicarbonate (NaHCO 3 ), Spongiacal® (Rheinkalk) or Sorbalit® (Märker scrubtechnik GmbH) are conceivable.
  • NaHCO 3 sodium bicarbonate
  • Spongiacal® Spongiacal®
  • Sorbalit® Märker scrubtechnik GmbH
  • the temperature for pollutant removal is preferably about 140-150 ° C.
  • activated carbon is also present in the circulating fluidized bed, in addition to which pollutants are adsorbed and separated from the exhaust gas.
  • a method for controlling the amount of the sorbent to be supplied is described, for example, in US Pat EP 1964602
  • the mass flow of the fresh feed sorbent is controlled as a function of the concentration of either the fresh sorbent or a sorbed contaminant or both in the recirculated solid.
  • the residual absorption capacity of the recirculated solid is taken into account and the consumption of sorbent can be kept minimal.
  • the concentration of either the fresh sorbent or a sorbed contaminant, or both in the recirculated solid is determined to be substantially continuous so that system changes can be reacted as rapidly as possible.
  • the determination is carried out by means of a Fourier transform near-infrared spectrometer (FT-NIR spectrometer).
  • FT-NIR spectrometer Fourier transform near-infrared spectrometer
  • the analysis can be carried out in situ .
  • the determination can be carried out using a solid sample taken from the circulation by means of a small cyclone. The determination is carried out batchwise. If the sampling takes place in short time intervals, a quasi-continuous determination can be carried out with this embodiment.
  • the pressure drop across the fluidized bed in the reactor can be monitored and the mass flow of sorbent recirculated into the fluidized bed reactor continuously controlled to maintain a constant inventory of bed material in the fluidized bed reactor.
  • the present invention also relates to an exhaust gas purification system for carrying out this method according to claim 8.
  • the exhaust gas purification system according to the invention comprises a first reactor and a downstream second reactor, wherein the first Reactor has a supply line for the exhaust gases and the second reactor leads a fresh sorbent feed line, and from the second reactor a channel for conducting the sorbent in the first reactor.
  • the first reactor of the exhaust gas purification system according to the invention is a fluidized bed reactor.
  • the pollutants contained in the exhaust gas are deposited by chemical reaction with the sorbent on the sorbent particles.
  • the first reactor of the exhaust gas purification system according to the invention has a device for injecting water.
  • the temperature can be controlled in the first reactor and the Schadstoffsorption be improved.
  • the second reactor of the exhaust gas purification system according to the invention is a fly-flow reactor, in particular a downpipe reactor.
  • the downcomer or entrained flow reactor leads to an optimal mixing of exhaust gases and sorbents and thereby improves the sorption of residual pollutants from the exhaust gases.
  • the fresh sorbent is supplied via a Venturi nozzle to achieve optimum mixing of sorbent and exhaust gases.
  • a calcium, sodium, mineral and / or carbon-based sorbent is used, for example, hydrated lime, sodium bicarbonate or a mixture thereof.
  • other sorbents or mixtures of several sorbents are conceivable, which include, for example, Spongiacal® or Sorbalit®.
  • the mass flow of the fresh supplied sorbent is controlled as a function of the concentration of either the fresh sorbent or a sorbed pollutant or both in the recirculated solid.
  • the exhaust gas purification system has an analysis device, in particular an FT-NIR spectrometer.
  • the exhaust gas purifier of the present invention may include a cyclone for taking samples of the recirculated solid, the analyzer preferably being connected to the cyclone.
  • the present invention also relates to the use of an inventive exhaust gas purification system for purifying exhaust gases from a waste incineration plant.
  • Waste gases generated during waste incineration usually contain various pollutants such as HCl, HF, SO 2 , nitrogen oxides or dioxin, as well as dusts.
  • HCl, HF, SO 2 and / or dioxin can be deposited with the advantages described above.
  • FIGS. 1 shows purely schematically an inventive emission control system.
  • the exhaust gas purification system 1 comprises a first reactor 2 in the form of a fluidized bed reactor, a second reactor 6 in the form of a downcomer reactor, and a solids separator 13 in the form of a fabric filter.
  • the first reactor 2 has substantially the shape of a hollow cylinder, which tapers downwards rejuvenated.
  • the first reactor 2 has a feed line 15, via which exhaust gases to be purified are introduced into the first reactor 2.
  • the sorbent located in the first reactor 2 is entrained by the exhaust gases flowing into the first reactor 2 and forms a circulating fluidized bed (not shown).
  • a channel 3 opens.
  • the first reactor 2 has in its lower, tapered region 17 a water nozzle 4, via which water can be injected into the first reactor 2. By injecting water, the temperature can be controlled in the first reactor 2 and the Schadstoffsorption be improved.
  • the upper end of the first reactor 2 is connected by a connecting channel 5 to a funnel-shaped inlet region 7 of the second reactor 6. Through this connection channel 5, the exhaust gases from the first reactor 2 are introduced into the second reactor 6. In this case, spent sorbent passes from the first reactor 2 into the second reactor 6.
  • the second reactor 6 comprises a sorption region 18 situated below the inlet region 7, which essentially has the shape of a hollow cylinder, which tapers upward, towards the inlet region 7, and downwards conically.
  • the second reactor 6 has at the upper end of the inlet region 7 a supply line 16 for fresh sorbent in the form of a Venturi nozzle.
  • exhaust gases and sorbents are mixed.
  • a downwardly inclined channel 8 leads away.
  • the purified exhaust gases are passed from the second reactor to the solids 13.
  • the solids separator 13 which comprises a plurality of individual filters, solids contained in the exhaust gas are separated off.
  • the emission control system 1 Above the Feststoffabscheiders 13, the emission control system 1 to an outlet 14 through which the purified exhaust gases are removed from the emission control system 1.
  • the sorption area 18 of the second reactor 6 has at its lower end an outlet 10, which is connected to the channel 3 for the passage of the sorbent in the form of a solid groove.
  • the solids channel runs obliquely downwards in the direction of the first reactor 2.
  • a portion of the sorbent from the second reactor 6 passes through the outlet 10 from the second reactor 6 in the solids channel and is at least partially passed through this in the first reactor 2 due to gravity.
  • Another part of the sorbent passes through the channel 8 into the solids separator 13 together with the purified waste gases and is collected in a filter bunker 9 running obliquely downwards.
  • the filter bunker 9 is also connected in its lower region with the solid groove 3.
  • the channel 3 has an outlet 12 with a rotary valve, via which excess and spent sorbent can be removed from the emission control system 1 together with the remaining separated solids.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Environmental & Geological Engineering (AREA)
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  • General Engineering & Computer Science (AREA)
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  • Biomedical Technology (AREA)
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  • Treating Waste Gases (AREA)

Claims (11)

  1. Procédé de nettoyage de gaz d'échappement par un procédé de sorption par voie sèche ou quasi sèche, dans lequel on introduit les gaz d'échappement dans un premier réacteur (2) et on les conduit du premier réacteur (2) dans un deuxième réacteur (6) qui suit et on ajoute un agent de sorption frais d'abord dans le deuxième réacteur (6) et on le conduit du deuxième réacteur (6) au moins en partie dans le premier réacteur (2), dans lequel le premier réacteur est un réacteur à lit fluidisé, dans lequel l'agent de sorption se trouve sous la forme d'une couche fluidisée circulante, et le deuxième réacteur (6) est un réacteur à flux entraîné.
  2. Procédé selon la revendication 1, caractérisé en ce que l'on pulvérise de l'eau dans le premier réacteur (2).
  3. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le deuxième réacteur (6) est un réacteur à tube de descente.
  4. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on conduit les gaz d'échappement du deuxième réacteur (6) à un séparateur de matières solides (13).
  5. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on ajoute l'agent de sorption frais par une tuyère de Venturi.
  6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on utilise un agent de sorption à base de calcium, de sodium, minérale et/ou de carbone.
  7. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que l'on régule le flux massique de l'agent de sorption frais ajouté en fonction de la concentration soit de l'agent de sorption frais soit d'un polluant sorbé ou des deux dans les matières solides recyclées.
  8. Installation de nettoyage de gaz d'échappement (1) pour le nettoyage de gaz d'échappement par un procédé de sorption par voie sèche ou quasi sèche, qui comprend un premier réacteur (2) et un deuxième réacteur (6) qui suit, dans laquelle le premier réacteur (2) présente une conduite d'arrivée (15) pour les gaz d'échappement et le deuxième réacteur (6) présente une conduite d'arrivée (16) pour un agent de sorption frais, et un canal (3) part du deuxième réacteur (6) pour conduire l'agent de sorption dans le premier réacteur (2), dans laquelle le premier réacteur est un réacteur à lit fluidisé, dans lequel l'agent de sorption se trouve sous la forme d'une couche fluidisée circulante, et le deuxième réacteur (6) est un réacteur à flux entraîné.
  9. Installation de nettoyage de gaz d'échappement (1) selon la revendication 8, caractérisée en ce que le deuxième réacteur (6) est un réacteur à tube de descente.
  10. Installation de nettoyage de gaz d'échappement (1) selon la revendication 8 ou 9, caractérisée par un séparateur de matières solides (13) installé en aval du deuxième réacteur (6).
  11. Utilisation d'une installation de nettoyage de gaz d'échappement (1) selon l'une quelconque des revendications 8 à 10 pour le nettoyage de gaz d'échappement provenant d'une installation d'incinération d'ordures.
EP08000447.6A 2008-01-11 2008-01-11 Procédé et installation de nettoyage de gaz d'échappement Not-in-force EP2078555B1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
PL08000447T PL2078555T3 (pl) 2008-01-11 2008-01-11 Sposób i instalacja do oczyszczania gazów spalinowych
DK08000447.6T DK2078555T3 (da) 2008-01-11 2008-01-11 Fremgangsmåde og anlæg til rensning af røggasser
EP08000447.6A EP2078555B1 (fr) 2008-01-11 2008-01-11 Procédé et installation de nettoyage de gaz d'échappement
PCT/EP2009/000072 WO2009087100A1 (fr) 2008-01-11 2009-01-09 Procédé d'épuration d'effluents gazeux

Applications Claiming Priority (1)

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EP08000447.6A EP2078555B1 (fr) 2008-01-11 2008-01-11 Procédé et installation de nettoyage de gaz d'échappement

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EP2638952B1 (fr) * 2012-03-12 2022-07-13 Andritz Aktiebolag Procédé de contrôle d'un système de nettoyage à gaz par mesure d'un paramètre d'un matériau absorbant

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CN102228788B (zh) * 2011-06-24 2013-07-31 中国科学院过程工程研究所 一种烧结烟气脱除二氧化硫和二噁英的装置及方法
CN102588976A (zh) * 2012-02-28 2012-07-18 崔勇 垃圾热解消纳器
DE102013207724A1 (de) 2013-04-26 2014-10-30 Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. Verbrennungsanlage mit verbesserter Lüftung und zyklonartiger Brennkammer
WO2016035013A1 (fr) 2014-09-02 2016-03-10 Rizzo, Rocco Dispositif de filtrage pour la poussière et d'autres polluants
DE102015122230A1 (de) * 2015-12-18 2017-06-22 Graf Enviropro Gmbh Verfahren zur Abgasreinigung mittels eines Wirbelschichtströmungsreaktors
DE102016124706A1 (de) 2015-12-18 2017-06-22 Graf Enviropro Gmbh Wirbelschichtströmungsreaktor
US10161630B2 (en) 2016-12-01 2018-12-25 General Electric Technology Gmbh Systems and methods for testing flue gas cleaning systems
CN108144414B (zh) * 2018-02-05 2023-08-11 山东大学 一种粉末活性焦双循环流化床脱硫系统及方法
CN108144412B (zh) * 2018-02-05 2024-03-08 山东大学 粉末活性焦双循环联合臭氧氧化脱硫脱硝的装置及方法

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Publication number Priority date Publication date Assignee Title
EP2638952B1 (fr) * 2012-03-12 2022-07-13 Andritz Aktiebolag Procédé de contrôle d'un système de nettoyage à gaz par mesure d'un paramètre d'un matériau absorbant

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WO2009087100A1 (fr) 2009-07-16
DK2078555T3 (da) 2013-11-25
EP2078555A1 (fr) 2009-07-15
PL2078555T3 (pl) 2014-01-31

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